Ethylene polymerization with conditioned molybdena catalyst



Feb. 5, 1957 A, ZLETZ ETHYLENE POLYMERIZATION WITH CONDITIONED MOLYBDENA CATALYST Filed May 17. 1952 Piu apodera' of ethylene solution in a liquid reaction medium per volume of catalyst per hour will be maintained. The temperature of polymerization is maintained at about 230 C. and the total pressure of ethylene and solvent at about 1,000 p. s. i. g. The average residence time of reactants in the reactor 16 is between about 5 and 30 minutes. At the conclusion of the reaction period for any particular aliquot passing through the reactor, the reaction medium should contain, in solution from 0.2 to about percent, by weight, of polyethylene.

Catalyst slurry, polyethylene and unreactcd dense phase ethylene pass in admixture from the reactor 16 through line into a catalyst settler 26 maintained at substantially reaction temperature. The catalyst slurry settles in the catalyst settler 26 and is withdrawn as relatively thick slurry by pump through line is returned through said line into the reactor 16.

Ethylene in the reaction zone can be present in excess of the solubility of ethylene in reaction medium under reaction conditions. This excess ethylene, liberated from the reactor 16 and separated in catalyst settler 26, can be recycled by pump 29 through line 30 into a heat exchanger' 31 which customarily operates to cool the recycled ethylene and thereby maintain temperature control in the reactor, the polymerization reaction being exothermic. Alternate methods, for example cooling the feed before charging to the reactor, can be employed to maintain the temperature control.

Liquid reaction medium containing only a minor quantity of solid catalyst is decanted as an upper layer from the catalyst settler 26 and is iiowed through line 33 into catalyst filters 34a and 34h which are positioned in parlallel and are operated significantly at substantially reaction temperature. ployed to ensure the tiuidity of the reaction product. The product-containing liquid reaction medium flows from the said line 33 through parallel lines 35a and 35h and into the said lters disposed in said lines.

The filtrate is passed through line 36a or 36h and pressure reduction valve 37 into a cooler 38 and thence through line 39 into ethylene separator 40 which is usually operated at atmospheric temperature and pressure. Ethylene dissolved in the etiiuent liquid reaction medium is separated in the said separator t0 and is recycled. It is especially advantageous to recycle this ethylene as it has become highly purified by the preceding polymerization step.

The product slurry, being substantially free of solid catalyst and containing polyethylene precipitated in the separator at the said low temperature thereof, is removed from the separator 40 through line 4l "and is pumped by centrifugal pump d2 through line 4.3 and parallel lines 44a and 44h to either one or both of product filters 45a and 45b. The polyethylene is separated `as a filter cake in the said filters and is removed for drying, milling, or other subsequent treatment not shown. Liquid reaction medium is removed las filtrate from the ilters 45o and 5b and flows through parallel lines 46a and 465 and thence through line 47 to collector drum 4S, into which fresh reaction medium is introduced from a line 49. The content of low-molecular-weight by-product, that is soluble in the reaction medium at iiltering temperature, can be kept to a minimum by continuously withdrawing a portion of the medium through line S0, and separating the medium and the said by-product. After said separation by, for example, distillation means (not shown), the rened solvent is delivered to collector drum 4S. Liquid reaction medium is withdrawn from the collector 4S through line 51 into a dcaerator 52 and is then pumped by a pump 53 through line 54 and heater 55 into line 56. The heated liquid reaction medium ows from line 56 into line 24 and admixes therein with dense phase heated ethylene and, in such admixture, tiows into reactor 16.

These elevated temperatures are em A portion of the settled catalyst slurry that is recycled through line 23 to the reactor 16 is withdrawn from said recycle and passed through line 57 into parallel lines 58a and 58h and thence into a set of catalyst regenerators 59a and 59b disposed in parallel. The settled catalyst slurry is flowed from line 57 through valved line 58a into the regenerator 59a until an optimum volume of catalyst slurry is delivered into the regenerator. Catalyst slurry is then directed from the line 57 through valved line 581) into the regenerator 59h. The catalyst in the regenerators can be washed in a solvent, preferably the same liquid as is employed as reaction medium, both to recover very high molecular weight polymer deposited thereon and to free the surface of the catalyst. If the catalyst becomes coated with carbon or refractive polymer it can be oxidized with an oxygen-containing gas and subsequently be reduced in the Yfollowing manner. Hydrogen is tiowed through a line 60a into the regenerator 59a under a pressure between about atmospheric and 1000 p. s. i. g. and effects a reduction at a temperature between about 250 and 500 C. of spent or partially spent catalyst in the regenerator, restoring the molybdena to an active, subhexavalent condition. Excess hydrogen is released through vent 61a and can be recycled to the regcnerator system. In like manner, hydrogen is tiowed through line 60!) into the regenerator 59]; and catalyst is reduced to form a subhexavalent molybdena. The hydrogen is released through a vent 61b.

The regenerated catalyst is removed from regenerators 59a and 59b and owed through respectively lines 62a and 62b and line 63 into the heated reaction medium flowing through line 56. The catalyst is slurried with the heated reaction medium in the said line 56 and is introduced into admixture with dense phase ethylene in line 24 to form a solution introduced into the reactor 16.

It is understood that many variations can be made in the abovc process with respect to heat interchange, product treatment, catalyst regeneration and the like, and that other variants described elsewhere can be introduced in the process; for example, propylene can be in part or in whole substituted for the ethylene.

The practice of the process of the present invention leads to ethylene homopolymers of widely variant molecular weight ranges and attendant physical and mechanical properties, dependent upon the selection of operating conditions. The inventive process is characterized by extreme flexibility both as regards operating conditions and as regards the products producible thereby. Thus the present process can be effected over extremely broad ranges of temperature and pressure. The practice of the present process can lead to grease-like ethylene homopolymers having an approximate molecular weight range of 300 to 700, Wax-like ethylene homopolymers having an approximate specific viscosity (X) between about i000 and 10,000, and tough resinous ethylene homopolyrners having an approximate specific viscosity (X105) of 10,000 to more than 300,000. By the operation of the present inventive process it has been possible for the first time, so far as is known, to produce tough ethylene polymers having specific viscosities (X105) of Well over 100,000, and even over 300,000. ln addition, the process of the present invention can be employed to effect the copolymerization of ethylene with other polymerizable materials and particularly with propylene. Propylene alone has been polymerized, by the employment of the catalysts of the present invention, in low yield to extremely high molecular weight, rubber-like polymers, in addition to oils and grease-like solids. Other polymerizable materials such as n-butylenes, isobutylenes, acetylene, isoprene, etc., may be copolymerized with ethylene to a certain extent but the resultant polymers thus far produced closely resemble polymers obtained with ethylene alone.

An important feature or my process is the employment of a solid catalyst comprising essentially a gamma-alugeoogst-7* mina,1tita`nia, or zerconia base anda molybdenum-oxygen compound Ain a sub-hexavalentfstate, thelfpreferred' fexampleof the" latter vbeing reduced molybdenum oxide (M003). The relative proportions of base to supported molybdena is not critical and may be varied throughout a relatively wide range provided that each component is present in amounts of at least approximately 1%. Molybdeua alone, whether in reduced 'or unreduced state, is ineffective and likewise the gamma-aluminag or other support by itself is ineffective. The preferred molybdenaalumina weight ratios are in the range of about 1:20 to 1:1, or approximately 1:4. A large number of 'other common catalyst supports have been tested withv various amounts of molybdena and found to be ineffective. Like- Wise, other catalyst components recognized as equivalents for molybdenum oxide in hydrof'orming have been found ineffective in my process evenwhen supported on gammaalumina. I prefer to employ a conditioned aluminamolybdena catalyst composed of gamma-alumina base containing about l to 80%, preferably about 5 to 35%, or approximately 20%, of molybdena (or other compound of molybdenum and oxygen) supported thereon.

The gamma-alumina base of the catalyst may be prepared in any known manner and the molybdenum may likewise be incorporated in or deposited on the base in any known manner. Excellent results have been obtained with alumina-molybdenum catalysts of the type conventionally employed for effecting commercial hydroforming, the word fhydroforming being employed to mean processes of the type described in U. S. Letters Patents 2,320,147; 2,388,536; 2,357,332, etc. As hereinbefore mentioned, the support can consist of alumina, titania or zirconia. As set forth in considerable detail in my copending application Serial No. 223,641, the alumina base must be in gamma form and can be an activated alumina prepared from hydratedalumina, a gel type alumina base prepared by precipitating agelfrom an aluminum `salt solution, or a colloidal Vgel of the type prepared from aluminum metal. These bases are all effective as supports for the molybdena catalyst.

The porous catalyst bases, whether of alumina, zirconia or titania, should have surface areas in the rangeof 40 to 400 square meters per gram, as measuredby nitrogen or n-butane adsorption (BET-method). Thernolybdena or other molybdenum-oxygen compound, such as cobalt molybdate, may be incorporated in the catalystbase in .any known manner, particularly as described in my copending application. Cobalt molybdate catalystsrmay be prepared as described in U. S. 2,393,288; 2,486,361, etc. The catalyst can comprise appreciable amounts of zirconia or titania, especially when one or more of these oxides is employed as the support (U. S. 2,437,531-2). -Gxides of other metals such as magnesium, nickel, zinc,

chromium, Vanadium, thorium, etc., maybe present in minor amounts, below l weight percent and preferably below l weight percent of the total catalyst. The catalyst, however, should `bei substantially free from oxides of alkali metals and iron, the latter being tolerable up to about 1%, but the former being maintained at as low a figure as possible.

i have found that the so-called spent molybdena-alumina catalysts from naphtha hydroforming operations are highly active catalysts for the polymerization Vof ethylene. The spent molybdena-alumina catalysts actually contain a substantial proportion of sulfur derived by the reaction of the molybdenum component of the catalyst with sulfur compounds contained in the naphtha being Vhydroformed or with H28 produced by hydrogenation of sulfur compounds during hydroforming;l the evidenceY indicates that f a substantial proportion ofthe molybdenum in the spent catalyst Vis present as a sub-hexavalent molybdenum sulfide,"'probab1y mostlyflvloSa'.A By spent hydroforming catalyst it is intended todenote a catalyst-containing-cokelike hydrocarbon materials rand ,one which-[can be regenerated by the conventional methods to its active state for hydr'oforrnirig. When *a molybdena-alumina *catalyst whihvv has beenV employed 'fornaphth'a hydroforming has been regenerated many times it at last reaches a dead state from which it cannot be regeneratedf this dead" state is associated with the conversion Yof gamma-alumina in the catalyst to the low surface area alpha-alumina, as determined by X-ray diffraction analysis.

The alumina-molybdena catalystmust be conditioned or activatedbefore it is useful for effecting ethylene polymerization and the conditioning step vis of great importance. it appears that at least a part of the molybdenum-must-be presentiin the final catalyst in a subhexavalent condition. Since molybdenum is usually cornpositedwith vthe a-bsorpti-vealumina in the form of a hex'avalent molybdenum compound, such as MoOs' which can be produced by decomposition of ammonium paramolybdate, it is necessaryto subject a catalyst to the Vconditioning or reducing'step'beforerit is effective foi-catalyzing ethylene polymerization. The conditioning or reducing step is preferably' effected with hydrogen although other reducing gases such as carbon monoxide, mixtures of hydrogen and carbon monoxide (water gas, synthesis gas, etc.), sulfur dioxide, hydrogen sulfide, etc., may be employed. The temperature ot' vthe conditioning step should be higher than about 400 C., the best conditioning temperature usually being in the range of about 400 to about 500 C., and in any case usually not higher than about 650 C. The hydrogen partial pressure in the conditioning step may range from ordinary pressure to 3000 p. s. i. g. or more, but for practical purposes is usually in the range of about 50 to 500, e. g. about 200 p. s. i. g. The time required for the conditioning step is dependent upon the particle size of the catalyst and its molybdenacontent. With a particle size of about 4to 6 mesh, a molybdenum oxide content of about 7.5% at vshorter timesv of conditioning are required even tothe extent that a maximum effective conditioning period will exist for a'powdered, or finely divided, catalyst. Thus, good activation Yof powdered catalyst containing 34% molybdena was obtained Vin l5 seconds, while this short time effected only fair conditioning of powdered catalyst containing 28% molybdena and was ineffective (apparently too long) for conditioning a catalyst containing 7.5% molybdena. For large particle sizes of the order of 2 to 6 rneshrcontaining 7.5 to 30% or more of molybdena, the optimum conditioning time lies in the range of about 15 seconds to l5 hours, although usually 6 hours is ample.

The conditioning treatment hereinabove described is required not only for fresh catalyst, but is also required for catalyst which has become relatively inactive in the polymerization step. As will be hereinafter described, the polymer formed in the polymerization reaction must be continuously or intermittently removed from the catalyst particles, preferably by means of solvents, and it is usually necessary or desirable to ycondition a catalyst surface which has been thus freed to some extent from polymer before it is again employed for effecting polymerizationQ When catalyst can no longer be rendered sufciently active by simple removal of polymer and coudtioning With a reducing gas as hereinabove described, it may be regenerated by burning combustible deposits therefrom with oxygen followed by theconditioning step. It has been observed that the conditioning treatment necessary to eect reactivation of catalysts from which polymer producthas beenremoved can be ,effected at somewhatlower temperatures than wouldI be eiectiv'eV inthe initial conditioning of fresh catalyst 'p'rep'ar'atin`s.`

The catalysts, comprising essentially a sub-hexavalent molybdenum compound supported upon an adsorptive alumina, titania, or zirconia, can bc employed in forms and sizes heretofore conventional in hydroforming operations with these and similar catalysts, for example, as pellets of generally cylindrical, spherical, or other shapes, or even in the form of coarse lumps. Suitable catalyst pellets may range in size from about 2 to about 6 mesh per inch and are often of generally cylindrical shape, having dimensions, for example, of Vs inch long and ig inch diameter. Powdered catalysts are highly active but rapidly become coated with polymer; thus, when powdered catalysts are used, high selvent-to-cata lyst ratios such as 5-50 pounds of solvent per pound of catalyst should be employed in the reactor to yield lower viscosity and more soluble polymer and thus to effect efficient removal of the polymer.

The charging stock to the present polymerization process comprises essentially ethylene or propylene or mixtures thereof. The ethylene charging stocks may contain inert hydrocarbons, as in refinery gas streams, for example, methane, ethane, or propane. When the charging stock contains an ethylene and propylene mixture, both of these oletins contribute to the production of resinous high molecular weight products.

Oxygen in the said stock eects temporary poisoning of the catalyst but the catalyst can be reactivated by rcduction. Water in the form of steam effects an irreversible poisoning of molybdena-alumina catalysts, so that they cannot thereafter be reactivated by purging or reducing treatments alone.

in general, polymerization can be effected in the pres ent process at temperatures between about 75 C. and about 325 C. Increasing the polymerization temperature tends to reduce the average molecular weightV of the polymer produced by the process. lt is often desirable to select a polymerization temperature which is at least equal to the melting or softening point of the solid polymerization product. Usually polymerization is effected in the present process at temperatures between about 110 C. and about 275 C. or the preferred narrower range of 130-260 C. As will be noted from the specific examples hereinafter supplied, the conjoint use of polymerization temperatures between about 200 C. and about 250 C. and a liquid aromatic hydrocarbon reaction medium is highly desirable in producingethylene polymers having specific viscosities 105)1ranging on the average from about 10,000 to about 30,000 in continuous operations with relatively long on-stream periods and clean catalysts.

It has been found that the present process can be employed for the production of relatively high molecular weight ethylene heteroand homo-polymers at relatively low pressures. For example, at a polymerization pres sure of only about 1.100 p. s. i. g., ethylene has been converted in substantial measure, according to the present process, to a homopolymer having a specific viscosity (l05) of about 200,000. These results are astounding when it is borne in mind that in prior art processes for the thermal polymerization of ethylene (as described in U. S. Patent 2,153,553) or polymerization of ethylene in the presence of oxygen as the catalyst (U. S. Patent 2,188,465), pressures in excess of 30,000 p. s. i. g. lead to the production of ethylene polymers having relatively low molecular weight, such as 24,000, as determined by the Staudinger specific viscosity method. The process of `the present invention can be effected to some extent even at atmospheric pressure. The upper limit of polymerization pressure is dictated by economic considerations and equipment limitations and may be 10,000

p. s. i. g., 20,000 p. s. i. g., or even more. A generally useful and economically desirable polymerization pressure range is between about 200 and about 5000 p. s. i. g., preferably between about 500 and about 1500 p. s. i. g., e. g. about 1000 p. s. i. g.

The Contact time or space velocity employed in the polymerization process will be, selected with reference to the other process variables, catalysts, 'the specific type of product desired and the extent of ethylene conversion desired in any given run or pass over the catalyst. 1n general, this variable is readily adjustable to obtain the desired results. ln operations in which the ethylene charging stoel: is caused to ow continuously into and `out of contact with the solid catalyst, such as is described with reference to the drawing. suitable liquid hourly sparc `reloeities are usually selected between about 0.1 and about l0 volumes, preferably about .5 to 5 or about l to 2 volumes of ethylene solution in a liquid reaction medium per volume of catalyst. The amount of ethylene or other olefin in such solutions should be in the range of about e 30 percent by weight, preferably about 2 to l0 weight percent or, for example, about 4 to 5 weight percent, thus corresponding to the desired content of polymer in eluent medium. ln batch operations, operating periods of between about one-half and about l0 hours, usually bctween about l and about 4 hours, are employed and the reaction autoclave is charged with ethylene as the pressure falls as a result of the ethylene conversion reaction.

Ethylene can be polymerized in the gas phase and in the absence of a liquid reaction medium by contact with the molybdenum hydroformngtype catalysts employed in the present process. Upon completion of the desired polymerization reaction it is then possible to treat the catalyst for the recovery of the solid polymerization products, for example by extraction with suitable solvents. However, in the interests of obtaining increased rates of ethylene conversion and of continuously removing solid conversion products from the catalyst, it is desirable to eliect the conversion of ethylene in the presence of suitable liquid reaction media. The liquid reaction medium may also be employed as a means of contacting the ethylene with catalyst by employing the technique of preparing a solution of ethylene in the liquid reaction Ymedium and contacting the resultant solution with the polymerization catalyst. Usually it is preferred to em ploy inert liquid organic materials, particularly such hydrocarbons as benzene, toluene, xylenes, tetralin, and decalin, as reaction media in the present process.

The liquid reaction medium employed in the present process appears to perform a variety of functions, and to perform these functions in varying degrees depending upon the operating conditions, catalyst and identity of the medium. Thus, the liquid reaction medium appears to function as a solvent for the ethylene to bring the ethylene into the necessary contact with the catalyst surface or growing ethylene polymer chain. The liquid reaction medium may function to protect the growing vpolymer chain 'from chain breakers, such as reactioninhibiting impurities in the feed stock, polymer already formed upon certain parts of the Catalyst surface, etc. The liquid reaction medium serves to reduce the viscosity of `the solid polymer retained upon and within the catalyst and thus may facilitate the process of transferring ethylene where it .is needed. The medium dissolves some of the normally' solid product from the catalyst surface. The liquid reaction medium makes possible a solid-liquid interface in which the growing ethylene polymer chain may be oriented and from which it may react with ethylene supplied from solution in the medium or from the gas phase. St should be understood, however, that i am in nowise bound by the theoretical considerations herein advanced to explain possible modes of action of the inert liquid reaction medium.

The fact remains that the inclusion of the liquid medium in the polymerization reaction zone in contact with the `catalyst produces an unpredictable and often desirable change in the polymerization of ethylene conducive .:liquid reaction' medium is to increase substantiallyv the Mrate of ethylene polymerization.

`Various classes of individual hydrocarbons or their mixtures which are liquid and substantially inert under the vpolymerization reaction conditi-ons of' the present process can be employed. These reaction media, which are not necessarily equivalent, may `include,numerous aliphatic Iand aromatic hydrocarbons, aplarge number ot propylene polymer.

The liquid hydrocarbon reaction medium may be presl lent in .they polymerization reaction zone. in proportions of about 10 to about 99 percent by. weight based on the weight ofboth ethylene and reaction medium. The liquid4 hydrocarbon reaction medium is present in the -reac- Vtion zone as a distinct liquid phase.

At low ratios of ethylene to the hydrocarbon reaction medium, for example ratios between about l yand about 30 percent, temperature control during the course of the ethylene conrversion process can be `readily `accomplished owing to the presence in theV reaction zone of a large liquid mass hav-- ing relatively. high heat capaci-ty. The liquid hydrocarlbon reaction medium can, moreover, be cooled by indirect heat exchange inside or outside the reaction zone. The employment of low ethylene concentrations in the hydrocarbon reaction medium also results in a marked reduction in the rate of accumulation of solid polymers on the catalyst in continuous operations.

The liquid hydrocarbon reaction medium will act as a solvent carrierV for the polyoletn produced and will reduce or substantially eliminate the Vdepositi-ori of high molecular weight olefin on catalyst Surfaces. A concentration of polymer between about 0.2 and 5 `percent by weight of the reaction medium will provide a Vreadily ltransportable liquid, higher concentrations within the range, e. g. 2 to 4 percent `being preferred. Y

When these solutions or dispersions of polymer in hydrocarbon reaction medium 4are releasedY to Ia reduced, and preferably atmospheric, pressure, and-.are cooled Vto a Itemperature between and 40 C., and preferably v vabout. atmospheric temperature, the polymerfwill precipi- I? tate .orfscparate from the :reaction mediumrand can be wliiltere'd or otherwise removed from the liquid medium.

.The regeneration of partially spent catalyst by-treat- @ment/with hydrogen or other reducing 'agents lcan be 'eifectedunder the -same Vconditions employed for initial Y 'l activation of a'batch of fresh catalyst, but -it has been 1 yfoundpos'sible to use much milder condition-SA. e., lower ftemperatures and pressures.

A large series of batch polymerization testswere reported in' my copending "application and'illustrated the "effect of, (il) polymerization in'r'gas or liquid; phase, (2)

certain reaction mediums, (3) hydrogen `.activation of the f catalyst for various"periods, (4) `various:molybdena alumina catalysts; `I( 5) catalystgsize,` l (6)Y spent hydroformer* 'catalyst in use as a; polymerizationcatalyst,*(7) activation Vwith v'carbon "monoxide, fsulfur dioxide, land `the like,

f (8) poisoningwithA oxygen or-weiten (9) vvarying lthe Vmolybdenum content of -'thc-catalyst, vand! (l0) Vzirconia or thoriafadmixed fwith the molybdena oncalumina catalyst; For, purposes ofbrevit'yfLtheY report lof these runs is not 'repeated in this application.

lnla test'run with unsupported hydrogen-reduc'edrMoOs Y under the standardized condition-s ,employed in batch runs with benzene as the: liquid reaction medium, no ethylene pressure drop wasV observable-overa period of v4 hours i and no ethylene polymers couldv beso'lated. Molybdic acid powder failed -to catalyze solid polyethylenes'produc- AThe employment of a commercial MoS2-ZnO-lvIg-O hydrogenation catalyst at 127 C. and 1000 p. s. i. g. ethylene pressure yielded no solid ethylene polymerl although a sulfur-containing hydroforming catalyst was active. A

` commercial-h/l-oS2-ganiina A1203 catalyst was found to be :inactive for `the preparation of 'polyethylene when tested under standardized conditions in a batch reactor. The

employment of a hydrogen-activated 7% molybdenasilica gel catalyst produced only a. trace of sol-id product -fromV ethylene under the standardazed conditions employed in other batch runs. It would `also appear ythat Vthe alumina component of the catalyst is not effective Amerely because of its large surface `area or pore volume.

' about '1000 square meters per gram or even more and @and one at the `lowerV end of the, well.

con-tained a central-well provided with three ther-mocouples, viz., one :at the upper end, one at the middle, One-fourth `inch coppertubing waswound about the reaction tube and air orfrwater, was circulated therethrough for. temperature `control infthe reaction tube.v Two electricalV resistance coils were wound over the copper coils to provide heat.

: Theentire assembly was suitably lagged with insulating material. Innthe runs reported in `Table 2, the partial Ipressure of lethylenezwas maintained at 900 p. s. i. g. -For purposes of `comparisonfthe run numbers employed Vhereinl larefiden'tical with 51the run numbers employed in Y myf'saidpcopending application.

Table 1 C. 1 Space Y `Run f -rCatalyst ".-Liquid Polym. Press ure,.l Velocity 'Resmfgnyspxl waGrease, y Remarks N o. Temp, p. s. 1. g. (g.feed/ ,en g..

. Y g;eat./hr.)

Time o cuts: 1 O i f 16 8,600 (11).-. .y 8.9 (u) after 1 hour; 54 52 .3M O }Benzene 1 255 1,000 3,8 25 7,700 (b)..- Y 0.0 (b) after 2%hou1s- 0 3 A 4 7,30o(c 4.0 roafter 3% hours.

' Y A] O 0.7 9,600 (a) 2.2 (a.) .Polymer removed 55.. {7 52 SMOG ..}Benzene.. i 150 800 g. 1.6 wit liq. 'reaction f S aanv 45,500 (11).. ny (b) Polymerremaining l y.o u. catalyst.

Total reactionperlod 'wassl hours.

area51? y tained at the top of the reactor and substantially the only ethylene entering into contact with the catalyst was that in solution in the benzene. Solid polymer was produced and was collected `in three fractions from the benzene reaction medium, as shown in Table l. On opening the reactor upon completion of the run, the catalyst was found to be free of accumulated polymer with the er:- ception ofthe iirst 2 inches of the catalyst bed, which may have been above the benzene level. The conversion of ethylene to solid polymer in this run was 36 weight percent. Substantially higher molecular weight ethylene polymers can be obtained by reducing the reaction temperature from 255 C. to a somewhat lower temperature of about 200 C. or 225 C.

In Run 55 the reaction temperature was reduced to 150 C., which was somewhat too low for continuous operation since an extremely high molecular weight polymer was formed which plugged the reactor.

ln Table 2 are presented data obtained during the continuous polymerization of ethylene by downow of ethylene and solvent through a hydrogen-activated commercial cobalt molybdate-alumina catalyst containing 3.28 weight percent CoO and 8.8 weight percent M003 (before hydrogen activation) supported on an active alumina. The liquid hourly space velocity of the ethylene-solvent mixtures in the runs of Table 2 was 2 to 2.5.

Table 2 only the rate of output was increased (compare Runs 57 and SS-A), but also the spe-cie viscosity of the product was more than doubled. A possible disadvantage of using a high feed concentration is that the rapid rate of production of high molecular weight polyethylene causes the catalyst to fragment from 1a-inch pellets to a fine powder. it has been found that the powder can simply be repelletted to produce an active catalyst. Between parts A and B of Run 58 hydrogen reactivation of the catalyst was effected at 850 F. and 300 p. s. i. g. hydrogen pressure, for about one-half hour. Run 58-A lasted 9 hours and 5ft-B about 71/2 hours. In part B of Run. 58, the temperature was raised to 270 C. As a result, the average specific viscosity fell sharply (38,100Xl0-5 in part A to l9,200 l05 in part B). Catalyst reactivation by hydrogen was practiced following Run Sii-B before the catalyst activity fell to the production rate of 2 grams of polymer per hour.

ln Run 59, benzene was substituted for xylene as the reaction medium, with consequent substantial increase in the average rate of polymer production despite the relatively low polymerization pressure and ethylene concentration which were employed. Catalyst regeneration or reactivation by hydrogen intervened between parts A and C of Run 59. The relatively low molecular weight of the polymer obtained in Run 59-C is due to the relatively high operating temperature of 260 C. It is of interest to note that the hydrogen from the reactivation treatment of the catalyst was allowed to remain in the reactor while feed was introduced in Run 59-C.

Run 56 COM'OOt/Aleos Q C Pressure, p. s. i-. Percent 02H; in Solvent Avg. nsp 105 Max. polymer outputy gjm-.[200 g. eat.. Hrs. 1.o (all to 2 g./hr.l200 g. eat .4... Total grams polymer produced before rate fell to 2 g./nr. Average rate of polymer production, gJhr Benzene.

rasoir l 19,00 4.5 i f ln Run 56-A, the catalyst activity at the end of 13 hours was 0.25 gram of polyethylene resin per hour per i 200 grams of catalyst. At this point the ethylene feed was discontinued and the catalyst was extracted with hot xylene, but no reactivation could be obtained in this manner. The catalyst was then treated with hydrogen for 3 hours at 850 F. and 500 p. s. i. g., which markedly reactivated the catalyst, as indicated by the results of Run :i6-C, which followed. The onstream period in Run i6-C was 22 hours. A comparison of Runs 56-C and 56-A indicates that the reactivation of the catalyst and the increase of ethylene concentration in the feed from 2 percent to percent resulted in the production Yof a higher specific viscosity polymer at a substantially increased rate of production.

Since hydrogcnation proved effective forcatalyst regeneration, hydrogen was added with the charging stoel;

during Run 57, but proved ineffective in prolonging the lt was observed that a part of the life of the catalyst. ethylene was converted to ethane. Comparing Runs 57 and 56-C, it will be observed that reducing the reaction pressure reduced the average specific viscosity of Vthe polymer product and also the average rate of polymer output.

To increase the rate of output of polyethylene, the concentration` of the feed in Run 58 was raised from 4 to 7 percent. The data in Table 2 indicate that not Maximum initial conversion rates in the foregoing runs were between and 95 percent and over half of thc converted olefin was polymerized to solid polyethylene. The concentration of polyethylene in the reaction me- Y dium was therefore between about 1.0 and 4.0 percent.

A solution of 34% propylene and benzene was prepared and passed downwardly through a bed of molybdena-alumina catalyst which had been activated by hydrogen treatment at 453 C. and 150 p. s. i. g. hydrogen pressure for 11/2 hours before use. It was found that propylene was converted to the extent of less than 1% in this operation to produce a polymer having a low molecular weight.

A 20% solution in benzene of a mixture of 68% ethyleue and 32% isobutylene was contacted with cobalt molybdate-alumina catalyst at 154 C. and 1200 p. s. i. g. fora period of 107 minutes. Olen conversion exceeded From the benzene solvent there were recovered 1.4 grams solid polymer (1,sp l05=4l,600) and 5.5 grams liquid polymer. ln addition` 5 grams of solid polymer were extracted from the used catalyst. In a similar run, a 33% solution in benzene of a mixture of 50% each of ethylene and isobutylene was charged over cobalt molybdatealumina catalyst to effect more than 95% olefin conversion. There were obtained 4.7 grams solid polymers; (i1sp l05=34,800) and 32.6 grams liquid polymer. ln each case the solid polymers were very stiff but much Run No u Activationgwith H2:

` Ethylene conc. in Solvent, percent by wt Product. distribution, perce Ethylene cono. in Solv Pressure, p. s. i Space velocity V./V,/h1

. more soluble in boiling xylene` than polymers oisimilar specieyi'scosity derived ,from the i polymerization of ethylenealone. I Y

Table 3 is devoted to data obtained on flow polymerization of ethylene in solution inthe indicated aromatic .hydrocarbon solvents in contact with an 8% M003- 'gamma alumina catalyst. Run 61 was carriednout in nine runperiods asta lifetest, vwith hydrogen vreactivation of the. catalystbetween periods, except after periods C and E, lnlgeneral, it will be notedthat the activated Moos-A1203, 'catalyst was far less sensitive to variations inthe concentration of ethylene in the solvent medium than the cobalt molybdate-alumina catalysts. The yields of solid polyethyleneswere goodand specific viscosities were good atreaction temperatures not in excess of about 250 C. Y

. ln Run 6l, after each period of operation, except as otherwise indicated,.the vcatalystrwas leached of accumulated polymer by circulating the solvent medium therethrough andwas then reconditioned by hydrogen treatment. Pelleted catalyst of 6-14 ,mesh was employed. VWhen the catalystwas removed-from the reactor at the end of the life` test, `therewas no evidence of catalyst disintegration. Approximately one gram of solid polyethylene was produced per gramrof catalyst during the life. test and the polyethylenes were tough and flexible.

ing` materials, binders, etc, toeven a wider .extent than polyethylenes made by prior processes.

,"greases.A 'Ihepolyethylenes may be employed asv coat- Thepolymersproduced by the process of the ypresent inyentionvespecially the..polymers having high specific viscosities in excess of about 100,000X10-5, can be. blended with the conventional lower molecular weight polyethylenes to impart stiiness or exibility or other desired properties thereto. The Vsolid resinous products produced by the process of the present invention can, like wise, be blended in any desired proportions withV hydrocarbon oils, waxes such as parai-lin or petrolatum waxesr with ester waxes, withhigh molecular Weight polybutylenesgand with other, organic materials. Small 'porportions-between about .0l and l percent of the'variousI polymers of ethylene produced by the process of the .prescnt invention can be dissolved or dispersed in hydrocar- Abon lubricating oils to increase V. I. and to decreaseol consumption when the compounded oils are Vemployed in motors; larger amounts of polyethylenes may be compounded with oils of various kinds and for various purposes.

The products having specific viscosities of 50,000X 105 orirnore produced by the present invention, can be employed in small proportions to substantially increase the viscosity of fluent liquidhydrocarbon oils and as gelling Table 3.--Ethylene polymerization-110W reactor Catalyst Temp., C Time,v min. Solvent Temperature, oC Pressure, p. s. i Space velocity V./V./br Duration of run, min Ethylene conv. (olens), percen Total products, g

Alkylate t Solid Polyethylenes.. Avg. Conc. of Polyethylene by weight. nspXlO (Solid Polyethylenes) Benzene. 11

Run NO L lG Catalyst suizos-8% M003 Activation with Hr Temo, Time, min

Solvent Temperature, O

Duration of run, min Ethylene conv.(oleins), percent. Total products, g Product distribution, percent:

' Alkylate lolyalkylate and polymer-- Solid Polyethylenes.'

Avg. Conc. otPolyethylenes in Solvent (Calc.),fpercent by Weight. 7813x105 (Solid Polyethylenes) l5 Xylene 15.0

.The polymers: produced by the process of this invention can be subjected to such after-treatment. as maybe desired, .to fit them for particular usesfor to impart desired ,propentiesfhusg the polymers 'having specific viscosities betweenabout 8,000 X10-5. and 40,000X 10"5 and formingcommercial-type resins, can be extruded, mechanically milled, iilmedor cast or converted to Sponges or latices. ltI1tioxidants,-.-` stabilirers,l fillers, extenders, plasticizers piggn'sentsf,insecticides,ffungicides, etc. caribe incorporated agents'fonsuch oils. The solution of about l gram of an ethylene polymer produced by this invention, having,

specific'viscosityxl05 of about 50,000 in about ten v liters of xylenes ata temperature close to thevboiling fpoint produced an extremely viscous solution.

The polymers produced by the present process can be subjected to chemical modifying treatments, such as adialogenation, lhalogenation..followed Yby dehalogenation,

. ,ftsulfonatiom and.'othersreactions to which hydrocarbonsv in the polyethylenes or. in by-product alkylatesv or 75 maybe subjected.

'Having thus described my invention, I claim;

l. In a process of producing high-molecular-weight hydrocarbons from a gaseous olefin selected from the group consisting of ethylene, propylene and mixtures thereof, which process comprises bringing such gaseous olefin into contact with a liquid hydrocarbon reaction medium, contacting said olen and said medium with a solid activated catalyst which, before activation, comprises essentially a hexavalent molybdenum oxygen compound combined with a supporting material selected from the group consisting7 of alumina, titania and zirconia, which catalyst has been activated before use in polymerization by partially reducing said hexavalent molybdenum oxygen compound when present on said supporting material by heating to a temperature between about 100 and 650 C. in the presence of a reducing gas, etfecting said contacting in a reaction zone at a temperature between about 75 and 325 C. under a superatmospheric pressure and converting gaseous olefin to polymer, and removing reaction mixture comprising liquid medium, solid catalyst, polymer, and unreacted olefin from the reaction zone, the improved method of operation which comprises separating solid catalyst from at least a portion of the reaction mixture while maintaining the said portion at a temperature between about 75 and 325 C. and under a pressure substantially equivalent to the employed polymerization pressure, iiowing separated reaction mixture substantially free of solid catalyst into a zone of reduced pressure, thereafter cooling separated reaction mixture to a temperature between about 0 and 40 C., and separating high molecular weight hydrocarbons deposited by the liquid reaction mixture upon said cooling and pressure reduction.

2. The process of claim 1 in which the selected gaseous olefin is ethylene.

3. The process of claim l wherein said material is alumina.

4. In a process of producing high molecular weight olefin polymers from a gaseous olefin selected from the group consisting of ethylene, propylene, and mixtures thereof, which process comprises introducing a gas containing a selected olefin and a liquid hydrocarbon reaction medium into Contact with a solid activated catalyst which, before activation, comprises essentially a hexavalent molybdenum oxygen compound combined with a t.

supporting material selected from thegroup consisting of alumina, titania and zirconia, which catalyst has been activated before use in polymerization by partially reducing said hexavalent molybdenum oxygen compound when present on said supporting material by heating to a temperature between about 400 and 650 C. in the presence of a reducing gas, maintaining liquid .reaction medium, absorbed olefin, and molybdena catalyst in a reaction zone at a temperature between 130 to 260 C. under a pressure of atmospheric to 5,000 pounds per square inch gauge for a time sufficient to convert a substantial portion of the olen to polymer, and removingY a reaction mixture comprising a liquid medium, solid catalyst, unreacted olefin, and polymer from the reaction zone, the improved method of operation which comprises settling out a dense slurry of solid catalyst from the reaction mixture at reaction temperature and pressure, ref cycling settled slurry to the reaction zone, fiowing liquid reaction mixture from the settling step to a filtering zone, filtering solid catalyst particles from reaction mixture at a temperature between about 75 and 325 C. and under a pressure substantially equivalent to the employed polymerit/.ationl pressure, owing filtrate therefrom into a zone of reduced pressure, cooling the ltrate to a temperature between about 0 and 40 C., and recovering high-molecular-weight olen polymer from the reaction mixture from which the said polymer is separated by the said cooling and pressure reduction.

5. 1n a process of producing normally solid olefin polymer from a gaseous olefin'selected from the group consisting of ethylene, propylene, and mixtures thereof, which process comprises incorporating a selected gaseous olefin in a hydrocarbon reaction medium selected from the group consisting of benzene, toluene, the xylenes, tetralin and decalin, introducing the said medium containing absorbed olefin into Contact with a solid activated catalyst which, before activation, comprises essentially molybdenum trioxide combined with a supporting material kselected from the group consisting of alumina, titania and zirconia, which catalyst has been activated before use in polymerization by partially reducing said molybdenum trioxide when present on said supporting material by heating to a temperature between about 400 and 650 C. in the presence of a reducing gas, effecting said contact under a pressure between about 200 and 5,000 pounds per square inch gauge and at a temperature between about 130 and 260 C. and maintaining said contact for a time sutiicient to convert at least a substantial portion of the olefin to polymer and provide a concentration of the so-formed polymer in the reaction medium of between about 0.2 and 10.0 percent by weight based on the weight of the said medium, and removing reaction mixture comprising liquid medium, solid catalyst, unreacted olefin and polymer, from the reaction zone, the improved method of operation which comprises separating solid catalyst from reaction mixture at a temperature between about 130 and 260 C. and under a pressure substantially equivalent to the employed polymerization pressure, flowing separated reaction mixture substantially free of solid catalyst into a zone of reduced pressure, cooling the reaction product to a temperature between 0 and 40 C.. and recovering olefin polymers that have separated from the cooled reaction mixture.

6. in a process of producing normally solid olefin polymer from a gaseous olefin selected from the group consisting of ethylene, propylene, and mixtures thereof, which process comprises incorporating a selected gaseous olefin in a hydrocarbon reaction medium selected from the group consisting of benzene, toluene, the xylenes, tetralin, and decalin, introducing the said medium containing absorbed olefin into contact with a solid activated catalyst which, before activation, comprises essentially a hexavalent molybdenum oxygen compound combined with a supporting material selected from the group consisting of alumina, titania and zirconia, which catalyst has been activated before use in polymerization by partially reducing said hexavalent molybdenum oxygen compound when present on said supporting material by heating to a temperature between about 400 and 650 C. in the presence of a reducing gas, effecting said contact under a pressure between about 200 and 5,000 pounds per square inch gauge and at a temperature between about 130 and 260 C. and maintaining said contact for a time sufficient to convert at least a substantial portion of the olefin to polymer and provide a concentration of the sci-formed polymer in the reaction medium of between about 0.5 and 5.0 percent by weight based on the weight of the said medium, and removing reaction mixture comprising liquid medium, solid catalyst, unreacted olefin and polymer, from the reaction zone, the improved method of operation which comprises settling out the dense slurry of solid catalyst from the reaction mixture at reaction temperature and pressure, recycling settled slurry to the reaction zone, withdrawing a portion of the settled catalyst slurry from the recycle, regenerating cata` lyst contained in the said withdrawn slurry, recycling regenerated catalyst to the reaction zone, flowing liquid reaction mixture from the aforesaid catalyst settling step to a filtering zone, filtering solid catalyst particles from reaction mixture at a temperature between about and 325 C. and under a pressure substantially equivalent to the employed polymerization pressure, fiowing filtrate therefrom into a zone of reduced pressure, cooling the filtrate to a temperature between about 0 and 40 C., and recovering high-molecular-weight olefin polymer from the reaction mixture from which the said polymer is separated by the said cooling and pressure reduction.

7. The process of claim 6 wherein the said withdrawn portion of settled' catalyst slurry is Washed to remove high molecular Weight polymer with an aromatic hydrocarbon, and is subsequently treated with hydrogen at a pressure between about atmospheric and about 1000 Referer-lees Cited in the tile of this patent UNITED STATES PATENTS Krase et al Mar. 19, 1946 

1. IN A PROCESS OF PRODUCING HIGH-MOLECULAR-WEIGHT HYDROCARBONS FROM A GASEOUS OLEFIN SELECTED FROM THE GROUP CONSISTING OF ETHYLENE, PROPYLENE AND MIXTURES THEREOF, WHICH PROCESS COMPRISES BRINGING SUCH GASEOUS OLEFIN INTO CONTACT WITH A LIQUID HYDROCARBON REACTION MEDIUM, CONTACTING SAID OLEFIN AND SAID MEDIUM WITH A SOLID ACTIVATED CATALYST WHICH, BEFORE ACTIVATION, COMPRISES ESSENTIALLY A HEXAVALENT MOLYBDENUM OXYGEN COMPOUND COMBINED WITH SUPPORTING MATERIAL SELECTED FROM THE GROUP CONSISTING OF ALUMINA, TITANIA AND ZIRCONIA, WHICH CATALYST HAS BEEN ACTIVATED BEFORE USE IN POLYMERIZATION BY PARTIALLY REDUCING SAID HEXAVALENT MOLYBDENUM OXYGEN COMPOUND WHEN PRESENT ON SAID SUPPORTING MATERIAL BY HEATING TO A TEMPERATURE BETWEEN ABOUT 400* AND 650*C. IN THE PRESENCE OF A REDUCING GAS, EFFECTING SAID CONTACTING IN A REACTION ZONE AT A TEMPERATURE BETWEEN ABOUT 75* AND 325*C. UNDER A SUPERATMOS- 